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CORROSION EVALUATION

L VP-HX-00001 Catalytic Oxidizer Heat Recovery Exchanger

ISSUED BY RPP-WTP PDC

24590-LA W-Nl D-LVP-00005 Rev. 3

Contents of this document are Dangerous Waste Permit affecting

Results

Materials Considered: Materials Considered Acceptable Materials

(UNSNo.) Type 304L (S30403) Type 316L (S31603) Type 347 (S34700) x AL-6XN® 6% Mo alloy (N08367) Hastelloy® C-22® (N06022)

Recommended Material Types: Structural support: Type 34 7 stainless steel

Hot side plates: Type 347 stainless steel

Cold-side components and enclosure: Type 347 stainless steel

Minimum Corrosion Allowance: 0.010 inch (structural steel in contact with offgas) No corrosion allowance required for heat transfer surface

Inputs and References • Operating temperature, cold-side (0 f) (norm/max): 169/ 189 (in); 370/412 (out) (24590-LAW-M4E-LOP-00009) • Operating temperature, hot-side (0 f) (norm/max): 624/680 (out); 724/792 (in) (24590-LA W-M4E-LOP-00009) • Corrosion allowance (in contact with offgas, excluding heat transfer surfaces): 0.010 inch (24590-WTP-SRD-ESH-01-001-02) • Corrosion allowance (heat transfer surfaces): 0.00 inch (24590-WTP-GPG-M-047) • Location: room L-0304f; out cell (24590-LAW-Pl -POIT-00005) • Operating conditions are as stated in the applicable section of WTP Process Corrosion Data - Volume 4 (24590-WTP-RPT

PR-04-0001-04)

Assumptions and Supporting Justification (refer to Section 19-References) Operating conditions presented on the Process Corrosion Datasheet (PCDS) are conservative with respect to corrosion.7

Operating Restrictions Develop a procedure for decontamination.

• Develop procedure to control lay-up and storage (mitigation of condensation in accordance with Manual - Operation, Maintenance And Installation Instructions For LAW Thermal Catalytic Oxidizer I Reducer (TCO) And Ammonia Dilution Skid, 24590-CD-POC-MBT0-00007-05-00004); including both before plant is operational and during inactive periods during plant operation.

• Procedures are to be reviewed and accepted by MET prior to use.

Concurrence......_ ),.,~A.c Opt!rations

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Incorporate revised PCDS Revise Ops Restrictions

Update references Add AEA notice

Incorporate revised PCDS Update design temp/pressure

Include AEA notice Minor format and editorial chan es

0 3/ 19/08 Initial Issue

REV DATE REASON FOR REVISION

Sheet: 1of15

DLAdler

DLAdler

DLAdler ORIGINATE

JRDivine RB Davis TErwin

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RB Davis DJWilse

JRDivine RB Davis SWVail CHECK REVIEW APPROVE

24590-LA W-NID-L VP-00005 Rev.3


Please note that source, special nuclear and byproduct materials, as defined in the Atomic Energy Act of 1954 (AEA), are regulated at the U.S. Department of Energy (DOE) facilities exclusively by DOE acting pursuant to its AEA authority. DOE asserts, that pursuant to the AEA, it has sole and exclusive responsibility and authority to regu late source, special nuclear, and byproduct materials at DOE-owned nuclear facilities. Information contained herein on radionuclides is provided for process description purposes only .

LVP-HX-00001: Sheet: 2of15

This bound document contains a total of 15 sheets.


Corrosion/Erosion Detailed Discussion

24590-LA W-NID-L VP-00005 Rev. 3

The heat recovery exchanger raises the offgas temperature from LVP-ADBR-OOOOlA/B, us ing the hot offgas from the catalyst beds (LVP-SCR-00001 ).

I General/Uniform Corrosion Analysis

a Background General corrosion or uniform corrosion is corrosion that is di stributed more-or-less uniformly over the surface of a material without apprec iable localization. This leads to relatively uniform thinning on sheet and plate materials and general thinning on one side or the other (or both) for pipe and tubing. It is recognized by a roughening of the surface and usually by the presence of corros ion products. The mechanism of the attack typically is an electrochemical process that takes place at the surface of the material. Differences in composition or orientation between small areas on the metal surface create micro-anodes and cathodes that facilitate the corrosion process.

b Component-S~cific Discussion Off gas corrosion, like atmospheric corrosion, depends on the development of corrosion cells or electrochemical cells consisting of the base metal , corrosion products, deposition products, anode, cathode, electrolyte, and current path . Stainless steels also have the added influence of the protective passive film . Because the corrosion process is electrochemical , an electrolyte must be presen t on the surface for corrosion to occur. In the absence of moisture, corrosion wi ll not take place. As an example, where temperatures are less than freezing, corrosion is minor because the ice is not a good conductor; or when the relative humidity is low, the water condensation is negligible and corrosion is negligible. Offgas corrosion is also influenced by the deposition of particulates, dust, and thin monolayers of gas constituents. The physically adsorbed molecules on the surface (HCI, HN03, and H2SO.) will form an ac id droplet from the deliquescence of water molecules . Moisture is needed to activate the corrosion process, typically a relative humidity of 60% to 80% is necessary to support corrosion; below this range corrosion does not occur. The relative humidity range for corrosion is discussed in Coburn (1978), Dean and Lee (1986), Dean and Rhea ( 1980), Schweitzer (1988), and in the ASM Metals Handbook, Volume 13. Normal operating conditions for the components of the thermal catalytic oxidizer (TCO) skid are dry, and relative humidity is very low (0.04% relative humidity, as shown in the PCDS). The anticipated dry-air conditions are not conducive to general corrosion and none is expected. Further, operating restrictions are in place to ensure that dry-air conditions are maintained.

The stabilized austenitic Type 347 stainless steel is considered suitable for the offgas conditions. The Type 347 austenitic stainless steel is an enhancement over that of a Type 300 stainless steel. The corrosion rates are a product of the alloy chemistry, and the only difference between Type 347 and Type 304L is the increase in carbon content that improves the high temperature properties. The carbon increase is offset with niobium and tantalum alloyed to decrease the tendency for carbide precipitation during fabrication and welding. Type 347 alloy has improved oxidation resistance and high temperature properties and is a good choice for the TCO components. Type 347 was selected fo r the following reasons: improved thermal properties, readily available in most product forms, standard stainless steel fabrication practice (tools and processes), and lower cost per pound than the higher nickel or duplex alloys (High-Temperature Characteristics of Stainless Steels, NIDI Publication No. 9004).

The recuperative heat exchanger is operated at elevated temperatures; oxidation is considered as part of this corros ion evaluation. The recommended alloy for the elevated temperature sections is Type 347 stainless steel. The higher carbon content and the addition of niobium to prevent sensit ization act to improve the oxidation resistance.

The skid base frame is not considered as a material in contact with the offgas. If structural materials are not welded to the pressure boundary of the heat exchanger, they are outside the scope of this corrosion evaluation .

2 Pitting Corrosion Analysis

Pitting is localized corrosion of a metal surface that is confined to a point or small area and that takes the form of cavities. Pitting corros ion will only be a concern if sufficient moisture is present. The heat exchanger normall y operates at temperatures above the dew point of the dry off gas, and therefore sufficient moisture is not present to act as an electrolyte for corrosion processes to proceed. It is assumed that there will be no condensation in the unit.

Justification for this position is that corrosion will not proceed without an electrolyte present .

3 Crevice Corrosion Analysis

Crevice corrosion is a form of localized corrosion ofa metal or alloy surface at, or immediately adjacent to, an area that is shielded from full exposure to the environment because of close proximity of the metal or alloy to the surface of another material or an adjacent surface of the same metal or a lloy. Crevice corros ion is similar to pitting in mechanism. Crevice corrosion will only be a concern if sufficient moisture is present. The off gas humidity is controlled so that there will be no condensation.

Justification for th is position begins with the understanding that thi s is an air handling unit operating at elevated temperatures, above the dew point. Corros ion will not take place or initiate when no electrolyte is present .

4 Stress Corrosion Cracking Analysis

Stress corros ion crack ing (SCC) is the cracking of a material produced by the combined action of corrosion and susta ined tensile stress (residual or app lied). In addition, sensitization of the gra in boundaries is prevented with the materials recommended. Either an "L" grade, low carbon, stainless steel or a niobium-stabilized stainless stee l is spec ified to negate sensitization from becoming a

LVP-HX-00001: Sheet: 3 of l5


24590-LA W-Nl D-L VP-00005 Rev. 3

corrosion issue. It is assumed that there will be no condensation in the unit; therefore, the recuperative heat exchanger will not undergo stress corrosion cracking because insufficient moisture will be present.

This position is justified because of the temperature of the gas during operation will be greater than the dew point. Corrosion will not take place or initiate when no electrolyte is present.

5 End Grain Corrosion Analysis

End grain corrosion is preferential aqueous corrosion that occurs along the worked direction of wrought stainless steels exposed to highly oxidizing acid conditions. End grain corrosion typically is not a major concern, it propagates along the rolling direction of the plate, not necessarily through the cross sectional thickness. In addition , end grain corrosion is exclusive to metallic product forms with exposed end grains from shearing or mechanical cutting. The heat exchanger design uses cooling channels and does not expose the pressure boundary cut ends to offgas. Also, end grain corrosion will not take place in the component because of the absence of sufficient moisture.

End grain corrosion is not expected to occur in the recuperative heat exchanger because the temperature of the gas will be greater than the dew point of the gas therefore corrosion will not occur in the absence of an electrolyte.

6 Weld Corrosion Analysis

The welds used in the fabrication will follow the WTP specifications and standards for quality workmanship. The materials selected for this fabrication are compatible with the weld filler metals and ASME/AWS practice. Using the welding practices specified for the project there should not be gross micro-segregation, precipitation of secondary phases, formation of unmixed zones, or volatilization of the alloying elements that could lead to localized corrosion of the weld.

This position is justified because the operating temperature and dry air conditions will not corrode because of the lack of the electrolyte for corrosion.

7 Microbiologically Influenced Corrosion Analysis

Microbiologically influenced corrosion (MIC) refers to corrosion affected by the presence or activity, or both, of microorganisms.

Typically, with the exception of cooling water systems and stagnant water, MIC is not observed in operating systems.

The recuperative heat exchanger will operate at elevated temperatures and the offgas is dry. In this system, the stated operating conditions are not suitable for microbial growth.

8 Fatigue/Corrosion Fatigue Analysis

Corrosion-fatigue is the result of the combined action of cyclic stresses and a corrosive environment. The fatigue process is thought to cause rupture of the protective passive film, upon which stainless steel can actively corrode in the localized area of the film rupture. The corrosive environment may also act to reduce the stress necessary for film rupture. The result is that a metal exposed to a corrosive environment and cyclic mechanical load may initiate cracking at conditions at stress levels less than the endurance limit for the material.

The recuperative heat exchanger is not cyclically operated; offgas flow is constant, steady and dry. Thermal cycles and therefore thermal stress is also low and associated with the start-up and shut down of the off gas system. Corrosion fatigue will not be observed in the recuperative heat exchanger (24590-LAW-MVC-L VP-00004, LVP-SKID-00002, LAW Thermal Catalytic Oxidi=er I Reducer, Stress Analysis with ANSYS).

The conclusion that corrosion fatigue will not be a problem is based on the low mechanical and thermal cycling, as well as the lack of an electrolyte for corrosion.

9 Vapor Phase Corrosion Analysis

Vapor phase corrosion considers the gas and vapor constituents that form acidic condensate and the alloy corrosion resistance. The aggressive constituents are HCl, HF, and HN03; however these are present in low concentrations in the gas. The formation of acidic condensate requires moisture condensing on the surface and mixing with the adsorbed surface constituents to produce an aggressive environment. Condensation on the surface is not likely during normal operation.

Vapor phase corrosion will not occur in the recuperative heat exchanger conditions because the operation conditions for this component preclude the presence of sufficient moisture and concentrations of acid gas forming components.

10 Erosion Analysis

Erosion is the progressive loss of material from a surface resulting from mechanical interaction between a particle and that surface . Solid particle erosion can occur in air, steam, and water fluid systems. The WTP waste is a slurry consisting of water, waste oxide particles, and I or precipitated salts. When the fluid propels the solid particles at a sufficient velocity and the particle mass is sufficient, the surface can be damaged by the combined effect of millions of individual erosion "scars". Prior to reaching the recuperative heat exchanger the offgas passes through a high effic iency particulate filter (HEPA) and therefore should be free of particulates.

The solids content and gas velocity are sufficiently low that erosion is not a concern.

LVP-HX-00001: Sheet: 4 of 15


11 Galling of Moving Surfaces Analysis

24590-LA W-NlD-L VP-00005 Rev. 3

Galling is a form of wear caused by a combination of friction and adhesion between moving surfaces . Under high compressive forces and movement, the friction temperatures cold-weld the two surfaces together at the surface asperities . As the adhesively bonded surface moves some of the bonded material breaks away. Microscopic examination of the galled surface shows some material stuck or even friction welded to the adjacent surface, while the softer of the two surfaces appears gouged with balled-up or tom lumps of material stuck to its surface .

Galling is most commonly found in metal surfaces that are in sliding contact with each other. It is especially common where there is inadequate lubrication between the surfaces. Softer metals will generally be more prone to galling; austenitic stainless steel is relatively soft and ductile and is known to gall easily. Martensitic sta inless steel or precipitation hardened stainless steel or nitrogen strengthened austenitic stainless steels have higher surface hardness and therefore are resistant to galling.

The recuperative heat exchanger does not have any moving surfaces.

12 Fretting/Wear Analysis

Fretting corrosion refers to corrosion damage caused by a slight oscillatory slip between two surfaces. Similar to galling but a much smaller movement, the corrosion products and metal debris break off and act as an abrasive between the surfaces, classic 3-body wear problem. This damage is induced under load and repeated relative surface motion, as induced for example by vibration. Pits or grooves and oxide debris characterize this damage, typically found in machinery, bolted assemblies and ball or roller bearings. Contact surfaces exposed to vibration during transportation are exposed to the risk of fretting corrosion.

The recuperative heat exchanger does not have moving parts and design precludes the use of tube support plates that would normally become a fretting corrosion problem in tube-and-shell heat exchangers. Fretting corrosion is not expected in this component.

13 Galvanic Corrosion Analysis

Galvanic corrosion is an electrochemical process in which one metal corrodes preferentially to another when both metals are in electrical contact, in the presence of an electrolyte. Dissimilar metals and alloys have different electrode potentials, and when two are in contact in an electrolyte, one metal acts as anode and the other as cathode. The electropotential difference between the dissimilar metals is the driving force for an accelerated attack. The potential difference for more than 200 mV is needed for sufficient driving force to make a difference. Galvanic compatibility is one of the attributes used to select the WTP alloys . Austenitic stainless steels in contact with other austenitic stainless steels do not have suffic ient electropotential difference to significantly influence the metal loss .

The recuperative heat exchanger plates, frame, and support materials are all fabricated from Type 347 stainless steel. In addition, the gas is dry and contains insufficient moisture to act as an electrolyte. Galvanic corrosion is not expected to be a corrosion issue under these conditions.

14 Cavitation Analysis

Cavitation corrosion is defined as another synergistic process, the combined influence of mechanical disruption of the metal surface and the corrosion of the active metal. Cavitation occurs when the local fluid pressure drops below the vapor pressure of the fluid resulting in a liquid vapor interface or bubbles to form. Their collapse on the metal surface has sufficient energy to rupture the oxide film and depending on alloy, may be capable of removing metal. The fluid chemistry and alloy define corrosion characteristics of the oxide film; where localization of the cavitation produces a condition where the bubble collapse rate is greater than the ability to passivate, the normally passive alloy can experience accelerated loss . This is most likely to occur in pumps, valves (flow control), orifices, ejectors/eductors, and nozzles .

Cavitation is not expected in an offgas system

15 Creep Analysis

Creep is defined as a time-dependent deformation at elevated temperature and constant stress, creep is a thermally activated process. The temperature at which creep beg ins depends on the alloy composition. Creep failures and stress rupture failures follow the same mechanism and are influenced by similar variables like temperature. Stress rupture is defined as bi-axial creep restricted to pipe like geometries . Creep is found in components subjected to heat for long periods and the creep rate generally increases as the temperature nears the melting point. The creep temperature is different for each alloy, the Nickel Development Institute has cataloged the creep properties of Type 304, Type 316, and Type 347 austenitic stainless steels (High-Temperature Characteristics of S tainless S teels). The material creep properties at 1000 °F indicate a difference of severa l hundred degrees over the maximum recuperative heat exchanger at 792 °F.

The maximum operating temperature for the recuperative heat exchanger is less than the creep temperature, creep will not occur.

16 Inadvertent Addition of Nitric Acid

Addition of nitric acid to the offgas is not a plausible scenario.

LVP-HX-00001: Sheet: 5of 15


17 Conclusion and Justification

24590-LA W-Nl D-L VP-00005 Rev. 3

The conclusion of this evaluation is that LVP-HX-00001 can be fabricated from Type 347 stain less stee l and that Type 347 stainless steel is capable of providing 40 years of service. Providing the reported dry-air conditions are maintained, Type 34 7 stainless steel is expected to be resistant to uniform and localized corrosion. The probable uniform corrosion is negligible; a minimum allowance of 0.010 inch for surfaces in contact with the offgas (except heat transfer surfaces) is recommended for conservatism. No corrosion allowance is recommended for the heat transfer surfaces. Conditions in the heat exchanger do not promote erosion so no erosion allowance is necessary.

18 Margin

Per 24590-WTP-SRD-ESH-01-001-02, Appendix H "When erosion and corrosion effects can be shown to be negligible or entirely absent, a design corrosion allowance need not be specified." In the reported dry-air conditions, there is no electrolyte. If there is no electrolyte, there can be no corrosion. The system is designed with a uniform corrosion allowance of0.010 inch based on the range of inputs, system knowledge, and engineering judgment/experience. The service conditions used for materials selection have been described above and result in negligible uniform loss. The specified minimum corrosion allowance exceeds the minimum required corrosion allowance which provides margin. The uniform corrosion design margin for the operating conditions is sufficient to expect a 40 year operating li fe and is justified in the referenced calculat ion.

Localized erosion of this component is not expected. Prior to reaching the recuperative heat exchanger, the offgas passes through a high efficiency particulate filter (HEPA) and, therefore, should be free of particulates. The solids content and gas velocity are sufficiently low that localized erosion is not a concern. Since localized eros ion effects are not present, additional localized corrosion protection is not required.

This component contains no fluids or electrolyte to promote localized corrosion. As shown in the PCDS summary table (page 8, below), the unit operates at high temperatures and low humidity (0.04% at the outlet) and is described in the PCDS. While not quantifiable, the largest contributor to the total local ized corrosion design margin is the absence of sufficient moisture to form a corrosive electrolyte. During inactive periods of plant operations and prior to initial plant startup, layup and storage procedures will monitor and control condensation.



19 References

24590-LA W-Nl D-L VP-00005 Rev.3

I . 24590-CD-POC-MBT0-00007-05-00004, Manual - Operation, Maintenance and Installation Instructions For LAW Thermal Catalytic Oxidizer I Reducer (fCO) And Ammonia Dilution Skid.

2. 24590-LA W-3YD-LOP-OOOO I, System Description For The Law Primary Offgas (LOP) And Secondary Offgas!Vessel Vent (L VP) Systems.

3. 24590-LA W-M4C-LOP-OOOO I, LAW Melter Ojfgas System Design Basis Flow sheets with ECCN 24590-LA W-M4E-LOP-00009. 4. 24590-LA W-MVC-LVP-00004, LVP-SKID-00002, LAW Thermal Catalytic Oxidizer I Reducer, Stress Analysis with ANSYS. 5. 24590-LAW-Pl-POIT-00005, LAW Vitrification Building General Arrangement Plan at El. 48 Feet - 0 Inches. 6. 24590-WTP-GPG-M-047, Preparation of Corrosion Evaluations. 7. 24590-WTP-RPT-PR-04-000 1-04, WTP Process Corrosion Data-Volume 4. 8. 24590-WTP-SRD-ESH-O 1-00 1-02, Safety Requirements Document Volume II. 9. ASM Metals Handbook, Volume 13 , Corrosion. 1987. ASM International, Materials Park, OH. IO. Coburn SK. 1978. Atmospheric Factors Affecting the Corrosion of Engineering Metals - STP 646. ASTM International , West

Conshohocken, PA 11 . Dean SW and Lee TS. 1986. Degradation of Metals in the Atmosphere - STP 965. ASTM International, West Conshohocken,

PA 12. Dean SW and Rhea EC. 1980. Atmospheric Corrosion of Metals - STP 767. ASTM International , West Conshohocken, PA 13 . NlDI. High-Temperature Characteristics of S tainless Steels, Publication No. 9004, Nickel Development Institute. Toronto,

Ontario, Canada. 14. Schweitzer PA 1989. Corrosion and Corrosion Protection Handbook. Marcel Dekker, Inc. , New York, NY.

Additional Reading

• 24590-LAW-MKD-L VP-00012, Mechan ical Data Sheet for 24590-LAW-MX-LVP-SKID-00002 24590-LA W-MX-LVP-00003 -LAW Cataly tic Oxidizer I Reducer.



24590-LA W-NID-L VP-00005 Rev. 3

PROCESS CORROSION DATA SHEET (extract}

Component(s) (Name/ID#) Catalytic Oxidizer Heat Recovery Exchanger (LVP-HX-00001)

Facility _L_A_w ____ _

In Black Cell? NO ------Stream ID

LVP14

Chemicals Unit Gaseous

C02 ppmV 22330

HCI ppmV 7

HF ppmV 4

NH3 ppmV 237

NO ppmV 35

N02 ppmV 0

S02 ppmV 7

S03(s) mg/m3 2

RH % 0 .04

Suspended Solids 'Wt"/o 0

Temperature •f 792

LVP-HX-00001: Sheet: 8 ofl5

24590-LA W-Nl D-L VP-00005 Rev. 3


24590-WTP-RPT-PR-04-0001-04, Rev. OA WTP Process Corrosion Data-Volume 4

Figure C- 25 LVP-HX-00001 Gaseous PCDS

Vessel : LVP _HX_ 1

Properties Susper·ded Solids [ffi %[

Total S81!S (Wt %~

Relative H umidit)' [% )

pH Anh·Foam Agont [ppmJ

TOC [kg/hi Preissure (bar)

Temperature [CJ Terrperal\re [FJ

Wmer FJcM· Rate [kgitlrJ Total PqJoous Flow Rate [kg.)-,~

Total Flow Rote [kq,lorj

GASEOUS JppmV or rn[)'m':J

Al C H31

0 2 co

C02 F2 H2

HCI

HCN HF 12

N2 NaCl( SJ

N::iCN SJ

NaF(;J Nol(SJ

NH3

NO N02

LVP26

0 0 C-0 nh.1

13.02 r/ a 0

2 70E.ffi 0 92 87.22 189.00 303 79 303.79

5.19E •OJ

8200 0 0

43·1

26053 0 0 9 0 5

699668 0 0 0 0 22

2 111 10

LVP14

0 ()00

!Va 0,04 fl/a 0

1.35E-OI 090

42222 W2.00 31SU5 319.15

62CE+03

8401 0 0 HI

2233)

0 0 7 0 4 0

7n673 0 0 0 0

m .35 0

Stream D LVP09

0 000 Na

1. 25 rva 0

1.JSE-04 0.90

21U1 41200 319.15

3'19. 15 620E•OJ

8401

18

22338 0

7 11 673 G G 0 G

'1925 1714

8 0 2 1&l778 190901 191317

P205(SI 0 0 0 P02 0 0 0

LVPIO

0 0 00

O.il<l fl!8

0 2.70E-OJ

0 92 360.00 600.00 303 79 303.?9

5 l9E .. 03 VI I VAPOR En€fgy

R..<>-co~'&)"tieat

ExctkirQ'!f Cold Cft!J:t$ O~ye

8256

43 1 26053

699669 0 0 0 0 22

2 111 10

13!lna

S02 10 7 7 10 S03!s) 0 2 2 0

Note: Concentratiom for constituents repre~enting particulates (a~ denoted by suffix"(~} .. in their name) are reported in units of mglm3; all others are reported in untts of ppmV

GENERAL NOTE FOR USE OF PCDS

LVP_HX_f

~£ 1"' tJ

• The information provided by the PCDS report is intended solely for use in support of the vessel material selection process and Corrosion Evaluations. The inputs, assumptions, and computational/engineering models used in generating the results presented herein are specific to this effort. Use of the information presented herein for any other purpose will require separate consideration and analysis to support justification of its use for the desired, alternative purpose.

• The process descriptions in this report cover routine process operations and non-routine (infrequent) process operations, when such exist, that could impact corrosion or erosion of process equipment

• The process descriptions provided in this report are for general information and reflective of the corrosion engineer 's analysis for transparency, the information is current only at the time this document is issued These process descriptions should not be referenced for design.


24590-LA W-NlD-L VP-00005 Rev. 3


6.6.1 Description of Vessel/Equipment


The LAW Secondary Offgas/Vessel Vent Process (L VP) System is designed to treat the offgas from the LA \V Primary Off gas Process (LOP) System and the LAW Facility Yessel Yen ts. The purpose of the L VP

System is to remoYe almost all remaining particulates. miscellaneous acid gases. nitrogen ox.ides. VOCs. and mercury from the LA \V Facility offgas that hm·e not been remoYed by the LOP system.

Figure I 0 is a sketch of the input and output a1Tm1gement of streams for all equipment within the L VP System. Streams that are not primary routes (infrequent transfers) are represented with dashed lines.

Figure lOb L VP System Sketch (detail of pertinent portion of system)

LVP09

,,,---: .-----____,.: LVP14--------

' '--------"

LVP26

LVP·ADBR-00001AIB

LVP-HX-OOOM LVP-HTR-00002

6.6.2 System Functions

The process functions of this system are as follows:

• Recei\·e LAvV Offgas from LOP System and LAW Facility Vessel Ventilation Streams

• Recei\·e Reagents Streams Such as Anunonia or Dilution Air to Ensure Offgas Component Destrnction

• Treat Offgas to Ensure Requirements are Met Before Erniniug to Atmosphere

• Transfer Offgas to Stack

• Transfer Liquid Effluents to RLD-VSL-00017.-'VB


24590-LA W-NID-L VP-00005 Rev. 3



These ve:,sels pe1form additiomil sy:, tem fimctions beyond the process fimctions. but these are outside the scope of this document . The non-process fonctions are not discussed any farther in this document. Howewr. they are listed below for completeness :

• Confme Hazardous Materials

• Flush System Components

• Rep011 System Data

6.6.3 Description of Process Functions

All process streams have been taken from Process Flow Diagrams 24590-LA W-M5 -V l 7T-00010 and 24590-LA \.V-P.!5-Vl 7T-0001 land associated drawing change notices (DCNs) 24590-LA W-M5N-Vl 7T-00012/ l 5/ l 7/29 and 24590-LA \V-M5N-Vl 7T-000 12/ 19i23/29, respectively. The P&IDs haYe also been looked at to obtain the most accurate flow diagram. These are as follmvs: 24590-LA \V-M6-LVP-00001001 / 1002 1 1003 I 1004 I 1005 I 1006 i 1001 I 2002 12003 / 2004 I 2005 / 2006 I 3001 ! 4001 / 4002 / 4003 I 5001 I 5002 and 24590-BOF-M6-A.MR-00002001 I 2002 I 300 1 I 3002 ! 5001. See Section 7 .1.3 for cotTesponding references in this section. A description of the process function of each piece of equipment is listed as follows:

Eauimnent Process Function

L VP-lL"{-00001 The heat recovery exchanger raises the offgas temperature from L \/P-ADBR-0000 lAIB. using the hot offgas from the catalyst beds (L VP-SCR-00001) .

6.6.3.1 Receipt Streams

The L VP system primarily receiYes LAW offgas from the LOP system and LAW Facility vessel ventilation streams. Other L VP system equipment receives various streams to help process tlle offgas.

The receipt streams for each piece of equipment are listed as follows. by \·essel. in order of process flow:

L VP-HX-00001 • L VP26 - Offgas from LVP-ADBR-OOOOlA/B

• L VP14 - Offga5 from LVP-SCR-0000 1

6.6.3.1.4 L VP26 - Off gas from L VP-ADBR-0000 IA/B

Stream L VP26 is the offgas from the adsorbers that enters the heat exchanger.

:\folarity KIA

Temperature The tempernnire of stream L VP26 will nonnally be 169"F (24590-LA W-M4C-LOP-OOOO 1. pg. 3 7. Cell Q33 . Ref 7.1.4(12)). The maximum temperatme is 189°F (24590-LAW-:M4C-LOP-00001. pg. 41. Cell Q33. Ref. 7. 1.4(12)) .

LVP-HX-0000 1: Sheet: 11 of l5

24590-LA W-NlD-L VP-00005 Rev. 3


Solids Concentration


The solids concentration for stream L VP26 will 1101111ally be near zero or trace solids.

Vapor Density The Yapor density of stream L VP26 will nonnally be 4.4 7E-2 lb/fr' to 4.02E-2 lb/ft3 (24590-LA W-M4CLOP-OOOO l. pg. 37. Cell A.I33: pg. 41. Cell Al33 . Ref. 7. 1.4(12)).

Liquid pH N/A

6.6.3.1.5 LVP14 - Offgas from LVP-SCR-00001

Stream L VP 14 is the off gas from the catalytic reducer that enters the heat exchanger.

Molarin• I /A

Temperatm·e The temperature of stl"eam L VP14 will normally be 724cf (24590-LA W-M4E-LOP-00009. pg. 11. Cell Q44. Ref. 7.1.4(13)) . The maximum temperature is 792°F (24590-LAW-M4E-LOP-00009. pg.. 15. Cell Q44, Ref. 7.1.4(13)).

Solids Concentration TI1e solids concentration for stream L VP14 will nonually be near zero or trace solids.

Vapor Density TI1e Yapor density of stream L VP 14 will nonnally be 2.27E-2 lb/ft3 to l.95E-2 lb/ ft3 (24590-LA W-M4ELOP-00009. pg.. 11. Cell AI44: pg. . 15. Cell AI44. Ref 7.1.4(13)) .

Liquid pH NIA

6.6.3.1.6 L VPlO - Offgas from L VP-HX-00001

Sn-eam LVP l 0 is the offg.as from the heat exchanger that enters the electric heater.

Molarin· N/A

T ernperamre The temperanire of stream L VPl 0 will nonnally be 624°F (24590-LA W-M4E-LOP-00009. pg. . 11. Cell Q36. Ref 7.1.4(13)). TI1e maximum temperature is 680 ' F (24590-LA\V-M4E-LOP-00009. pg. 15. Cell Q36. Ref. 7 .1.4(13)) .

Solids Concentration The solids concentration for stream L VP l 0 will nonnally be near zero or trace solids.

Vapor Densin· TI1e Yapor density of o,tream L \ lPlO will nomrnlly be 2.56E-2 lbift3 to 2.25E-2 lb!ff (24590-LAW-M4ELOP-00009. pg. 11. Cell AB6: pg.. 15. Cell Al36. Ref. 7.1.4(13)).

Liquid pH N/A


24590-LA W-NID-L VP-00005 Rev. 3



6.6.3.1.13 LVP09 - Offgas from L VP-SCR-00001 via LVP-HX-00001 to LVP-SCB-00001

This stream is the offga:; from the selectiYe catalytic reducer \·ia the heat exchanger to the scrubber.

:\folaritv NIA

Temperature TI1e temperatme wi ll nonnally be 3i0°F (24590-LAW-M4E-LOP-00009. pg. 11. Cell Q45. Ref. 7.1.4(13)). TI1e ma.\:imum temperature is 412°F (24590-LA W-l\.14E-LOP-00009. pg. 15. Cell Q45. Ref 7.1.4(13)).

Solids Concentration The solids concentration will nomially be near zero or trace solids.

Vapor Densitv TI1e Yapor density will nonnally be 3.27E-2 lb/ft3 to 2.84E-2 lb/ ft3 (24590-LAW-M4E-LOP-00009. pg. ll.CellAI44:pg.15.CellAI44.Ref. 7.1.4(13)).

Liquid pH N/A

6.6.3.2 Outlet Streams

The outlet streams for each piece of equipment are listed as follows . by yes:,el. in order of process flow:

L VP-HX-0000 1 • L VP 10 - Off gas from L VP-HX-00001

• L VP09 - Offg:as from L VP-SCR-00001

6.6.4 Process :\'lodes

6.6.4.1 :\"onnal Operations

Based on the assessment of streams frequently transferred in and out of the L VP System equipment. the following nonnal processing modes are considered:

L ·vP-HX-00001

• L VP26 - Offgas from L VP-ADBR-OOOOlA/B

• L VP 14 - Off gas from L VP-SCR-00001

• LVPlO - Offgas from LVP-HX-00001

• L VP09 - Off gas from L VP-SCR-00001

6.6.4.2 Infrequent Operations

None identified.


24590-LA W-NID-L VP-00005 Rev. 3



6.6.5 Summary of Processing Conditions for L VP System

6.6.5.1 :'.\ormal Operations

The following table summarizes the nonnal processing modes for L VP System equipment.

Stream NumbN· Wei2ht % lrDS Na :\'lolaritv Temperature (0 F)

nonnal upper nonnal upper nonnal upper

L 'VP-HX-00001

L VP26 (in) - cold 0 trnce n/a 1i/a 169 1S9 side

L VP 14 (in) - hot side 0 trace 1i/a n/a 724 792 L VP 10 (out) - cold 0 trace 1i/a n/a 624 680

side L VP09 (out) - hot 0 trace w'a n ia 370 412

side

6.6.5.2 Infrequent Operations

None identified.



24590-LA W-NID-L VP-00005 Rev. 3

24590-LA W-3YD-LOP-00001, Rev. 003 System Description for the LAW Primary Offgas (LOP) and Secondary OffgasNessel Vent (LVP) Systems

6.4.1.3 Catalytic Oxidizer/Reducer (L VP-SKID-00001 and L VP-SKID-00002)

The offgas has potentially high levels of NO, because the melter decomposes the parent nitrate/nitrite rompounds. Some of the resultant NO, is decomposed to nitrogen and water in the melter, and some is removed by scrubbing in the SBS. VOCs are also present in the offgas stream. Both the VOCs and the remaining NO, require removal.

The off gas is passed throµgh a catalytic oxidizer/reducer skid (L VP-SKID-00002) housing a heat recovery exchanger (LVP-HX-00001), an electric heater (LVP-JITR-00002), VOC catalyst (LVP-SC0-00001), and SCR catalyst (L VP-SCR-0000 l ) . The skid is located in room L-0304F at the 48-foot elevation and approximate dimensions for the skid are 36 ft long by 11 ft high by 8 ft wide. The heat recovery exchanger first raises the off gas temperature using the hot off gas from the catalyst beds. This heat exchanger is designed to be of a plate and frame design to eliminate the problems associated with tube to plate joints. The hot side of the heat exchanger cools the offgas prior to discharge from the skid. [ 4.3.3.17]

LVP-HX-00001 : Sheet: 15 of 15

tu~~~n - washington · influence of the protective passive film. because the corrosion process is...

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